EP0162085B1 - Procede de separation de gaz polluants acides et installation de combustion - Google Patents

Procede de separation de gaz polluants acides et installation de combustion Download PDF

Info

Publication number
EP0162085B1
EP0162085B1 EP19850900002 EP85900002A EP0162085B1 EP 0162085 B1 EP0162085 B1 EP 0162085B1 EP 19850900002 EP19850900002 EP 19850900002 EP 85900002 A EP85900002 A EP 85900002A EP 0162085 B1 EP0162085 B1 EP 0162085B1
Authority
EP
European Patent Office
Prior art keywords
sorbent
flue gas
combustion
gas stream
bag filter
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired
Application number
EP19850900002
Other languages
German (de)
English (en)
Other versions
EP0162085A1 (fr
Inventor
Ralf Lindbauer
Alfred Glasner
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Waagner Biro AG
Original Assignee
Waagner Biro AG
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Waagner Biro AG filed Critical Waagner Biro AG
Publication of EP0162085A1 publication Critical patent/EP0162085A1/fr
Application granted granted Critical
Publication of EP0162085B1 publication Critical patent/EP0162085B1/fr
Expired legal-status Critical Current

Links

Images

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/48—Sulfur compounds
    • B01D53/50—Sulfur oxides
    • B01D53/508—Sulfur oxides by treating the gases with solids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/68—Halogens or halogen compounds
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J7/00—Arrangement of devices for supplying chemicals to fire
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2215/00—Preventing emissions
    • F23J2215/30—Halogen; Compounds thereof
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2215/00—Preventing emissions
    • F23J2215/60—Heavy metals; Compounds thereof
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2217/00—Intercepting solids
    • F23J2217/10—Intercepting solids by filters
    • F23J2217/101—Baghouse type
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2217/00—Intercepting solids
    • F23J2217/40—Intercepting solids by cyclones
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2219/00—Treatment devices
    • F23J2219/60—Sorption with dry devices, e.g. beds

Definitions

  • the invention relates to the dry removal of the harmful gases and heavy metals from flue gases and in particular to a method for the two-stage separation of acidic harmful gases and heavy metals and their compounds from flue gases after combustion plants, such as.
  • the combustion of waste is one of the cleanest types of waste disposal, but has the disadvantage that a number of released pollutants such as. B. HCI, SO 2 , HF and heavy metals and compounds of the pollutants escape from each other.
  • a number of released pollutants such as. B. HCI, SO 2 , HF and heavy metals and compounds of the pollutants escape from each other.
  • HCI contents of approx. 1,000 mg HCI / Nm 3
  • more than 1,500 mg HCI / Nm 3 have already been measured in the exhaust gases.
  • the tolerance limit for new systems is 100 and for old systems 200 mg HCI / N m3.
  • FR-A-2 500 322 or DE-A-31 06 526 and DE-A-31 06 580 to clean at least a partial stream of the outflowing cleaned exhaust gas and wet it with the to reunite the partial stream that remained dry.
  • FR-A-1 424 831 discloses the possibilities of blowing a dry absorbent either into the combustion chamber or after the combustion chamber into the flue gas stream and separating it by cyclones, the separated dry dust being returned to the flue gas stream, at least partially, for better use of the absorbent. can be involved.
  • the invention has set itself the task of reducing the amount of chemicals in the dry separation of harmful gases, reducing the sorbent costs and also the landfill costs or stress on the landfills. It has been found that the heavy metal content of the exhaust gas is also reduced by the invention. Furthermore, the operational safety and the availability of the system are increased by the buffer effect of the second stage.
  • the process according to the invention is characterized in that the entire flue gas stream is cooled and the flue gas stream to be cleaned after the dry first cleaning in the temperature zone rich below 400 ° C is brought into contact with NaHC0 3 , CaO, Ca (OHh and / or Mg (OH) 2 , a second dusty, newly introduced sorbent, the remaining harmful gas is set off and finally the flue gas flow from the loaded sorbent in a second, preferably designed as a cloth filter, dry separator, which is operated at least 5 ° C above the water dew point of the flue gas.
  • the incinerator according to the invention is characterized in that in the area of the partially cooled flue gas between the electrostatic filter, cyclone or multicyclone (2) and a cloth filter (6) the second feed (12 ') is provided for a second sorbent with a chemical composition different from that of the first sorbent is. Further embodiments can be found in claims 9 to 11.
  • FIGS. 1 to 3 show the circuit diagram of a waste incineration plant
  • Fig. 2 shows a construction variant of a partial area to Fig. 1
  • Fig. 3 shows a sorbent feed in detail.
  • the combustion chamber 1 comprises a combustion chamber 1, into which the garbage-like fuel is introduced according to arrow 8.
  • the resulting flue gases are cooled on the downstream heating surfaces and cleaned in the dry separator 2, which is designed as an electrostatic filter, multicyclone or simple cyclone, and fed to a chimney 7 in a known manner via a suction fan 3.
  • two devices are provided for separating the pollutants, the first in the area of the combustion chamber 1 comprising a lime dust bunker 4, from which 10 lime dust with an average grain size of less than 20 ⁇ m is mixed with an air supply via a metering device, in which the air is admitted Blower 11 is blown into the combustion chamber for burning the fuel.
  • a plurality of sorbent feeds 12 are provided in the combustion chamber for uniform distribution and dispersion of the sorbent.
  • the lime is broken down into CaO and C0 2 in the combustion chamber, the CaO sorbing some of the pollutants, in particular HCl and S0 2 .
  • Any CaO not used by sorption of pollutants which is carried away by the exhaust gases into the heating surfaces of the boiler, absorbs the C0 2 present with a relatively high partial pressure when leaving the boiler in the low temperature range, so that CaC0 3 in the collecting line 9 in the fly ash , CaS0 3 and CaCI 2 can be detected.
  • the heavy metal inclusion in this area is very low, so that deposits of the dry separator 2 can be deposited without any problems.
  • the system described permits the cleaning of harmful gases in the order of magnitude of 66%, so that the exhaust gas leaving the dry separator 2 contains approximately 1/3 of the pollutants of the flue gases produced in the combustion system.
  • This pre-cleaned flue gas is now fed at a temperature of below 400 ° C to a second device, a second sorption stage, which is designed as a dry filter 6, in particular as a cloth filter, the exhaust gas prior to cleaning or in the cleaning room being a reactive sorbent such as e.g. B.
  • Ca (OH) 2 is mixed from a reservoir 5 via the line 12 'and feed lance 19. It is introduced with high dispersion so that practically every single grain can react.
  • the mean grain size is less than 10 wm and has a specific surface area that is greater than 3 m 2 / g (BET).
  • This reactive sorbent acts in the dry filter and absorbs the remaining pollutants, the sorbent metering 10 'or the feed 11' of the dispersing air being regulated according to the pollutant content in the chimney.
  • a sensor 16 and a corresponding measuring line 17 are shown. If the dry filter 6 is designed as a cloth filter with suspended filter bags 14, the dust-shaped, loaded and unloaded sorbent is deposited on the filter bags 14, whereby further pollutant sorption is achieved even if the fresh sorbent supply fails, so that the pollutant content of the flue gas is not fully reduced to Chimney emissions can penetrate.
  • the sorbent of the second stage can also be fed intermittently or intermittently upstream of the dry separator (cloth filter), since despite the dust which is also separated on the filter cloth, its reactivity is uniform over 1 1/2 hours maintains.
  • the sorbent feed in the second stage in front of the cloth filter can be added in batches once per cleaning cycle in one, which on the one hand improves the utilization of the second sorbent, on the other hand also represents a sorbent buffer effect for possibly fluctuating harmful gas contents from the first stage, and thirdly a technical simplification compared to a normally difficult, continuous dosing.
  • the loaded and unloaded sorbent deposited on them falls into a funnel arranged on the filter base and can be recirculated from this to the storage container 5 via line 15 for better utilization of the sorbent content.
  • the ground sorbent can for better and easier dispersion in the flue gas stream a grinding aid such.
  • B. CaC1 2 are added, so that the recirculation of the not fully used sorbent from the second stage in both the first and in the second stage, that is, in the reservoir 4 and 5, is appropriate.
  • a heating device 18 is provided in the dry filter 16, so that it is ensured is that the cloth filter is operated above the dew point in all operating phases.
  • FIG. 2 shows an embodiment variant of FIG. 1 for the second dry filter 6, in which the sorbent supply 12 'does not take place via a lance 19 but via the blower 3, which is arranged in front of the dry filter 6, the sorbent supply 12' preferably opens directly into the blower 3 or can be arranged before or after the blower.
  • This design variant has the advantage that the sorbent is finely dispersed by the action of the blower 3 or the inevitable eddy formation, which can improve the specific reactivity.
  • the heavy metal is mainly incorporated in the dry filter 6, so that in addition to the used sorbent (CaCl 2 and CaS0 3 ), the heavy metal compounds can also be found in the separated ash.
  • the fly ash obtained can be converted into a non-elutable mass by adding 15% cement and 42% water, which can also be deposited in a normal landfill.
  • FIG. 3 shows a lance 19 for the sorbent feed 12 ′, by means of which the sorbent feed can take place uniformly over the entire immersion cross section.
  • the following tables show test results on a waste incineration boiler with an hourly combustion output of 12 t, in which 60,000 m 3 of exhaust gas per hour are produced, which have a maximum HCI content of 1,500 mg / Nm 3 .
  • the tables are designed for a clean gas content of 200 mg HCI / Nm 3 , which corresponds to a total degree of separation of 86.7%.
  • the effect of a single-stage system in which the sorbent is only supplied in the second stage can be seen from the first line of each table.
  • the cleaning options for the first drying stage in the combustion chamber can be found in column 3 (HCI content between the first and second stages).
  • the required stoichiometry in the 2nd stage varies between 1 and 6.5 depending on the EBGD.
  • the consumption of sorbents is low in terms of cost if there is a degree of incorporation between 60 and 70% in the first stage by blowing in cheap lime, so that in order to achieve the guaranteed values in the second stage a degree of incorporation of 55 to 66% is necessary for more dense sorbent is. If, on the other hand, the amount of sorbent blown in is to be a minimum in view of the landfill that will later become necessary, the range is 50% integration in the first stage and 73.3% in the second stage, which means that annual sorbent consumption is 8,000 operating hours around 2,400 t is given. With an integration level of 60 or 70% in the first stage, this value increases to 2,700 or 3,300 t per year.
  • any combination can be used as sorbents: CaC0 3 , MgC0 3 . Na 2 C0 3 , NaHC0 3 , Ca (OH) 2 , Mg (OH) 2 , CaO, all of the above-mentioned sorbents being usable in the first stage and the four last-mentioned sorbents in the second stage.
  • An important selection criterion is the price of the sorbent used, which depends on the local conditions.
  • the aim of the dispersion in the individual cleaning stages is to strive for an individual grain dispersion, so that the specific surface area of the order of magnitude, depending on the grain size, of 1 to 3 m 2 / g is achieved.

Landscapes

  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • Biomedical Technology (AREA)
  • Environmental & Geological Engineering (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Treating Waste Gases (AREA)

Abstract

Afin de séparer les produits nocifs des fumées après des installations de combustion, on propose un procédé de sorption à deux étapes avec différents sorbants, par exemple du calcaire pulvérisé ou de l'hydrate de calcaire pulvérisé, dans différentes zones de température, par exemple 1000oC et 400oC, un refroidissement considérable des fumées entre les deux points d'alimentation en sorbants et une séparation du premier agent de sorption déjà utilisé étant considérées comme des pas importants, si bien qu'il y a diminution des coûts en agents de sorption et des quantités absolues de sorbants, ainsi qu'obtention d'un degré de séparation comparable à celui d'un procédé par voie humide. Un avantage essentiel est également donné par la séparation adéquate des métaux lourds dans la zone de l'agent de sorption avec volume minimum, ce qui contribue à abaisser les coûts de dépôt de déchets.

Claims (11)

1. Procédé de séparation à deux étages de gaz polluants acides, métaux lourds et leur combinaison des gaz de fumée d'installations de combustion telles qu'usines d'incinération d'ordures ménagères suivant lequel du CaC03 et/ou MgC03 pulvérulent sont introduits avec le combustible ou dans le courant de gaz de fumée chaud sortant du lieu de combustion avec l'air de combustion nécessaire dans la zone de la chambre de combustion à une température de plus de 700 °C et suivant lequel une partie du gaz polluant est fixé par le produit de décomposition pulvérulent ainsi que le produit de décomposition chargé est séparé du courant de gaz de fumée, caractérisé en ce que tout le courant de gaz de fumée est refroidi et le courant de gaz de fumée qui doit être purifié après la première purification sèche à une température de moins de 400 °C est mis en contact avec NaHC03. CaO. Ca(OH)2, un deuxième sorbant pulvérulent nouvellement introduit, et le gaz polluant résiduaire est lié et finalement le courant de gaz de fumée est purifié du sorbant chargé dans un séparateur sec, de préférence construit comme filtre en tissu qui est opéré à un température au moins 5 °C au-dessus du point de rosée de l'eau du gaz de fumée.
2. Procédé suivant revendication 1 caractérisé en ce que le deuxième sorbant a une surface spécifique plus large que 3 m2/g (BET) et/ou une grosseur de grain moyenne de moins de 10 ILm et qu'il est uniformément réparti sous forme de grains isolés sur la section de passage du moment au point de chargement dans le courant de gaz de fumée et dispersé à des vitesses entre 20 et 300 m/s.
3. Procédé suivant revendication 1, caractérisé en ce qu'un agent dispersant sous forme d'additif de broyage et/ou dessicateur de gaz tel que triéthanolamine et/ou CaC12 est ajouté au deuxième sorbant.
4. Procédé suivant revendication 1, caractérisé en ce que le deuxième sorbant est chargé dans le courant de gaz de fumée avant le filtre en tissu et en accord avec sa purification en discontinu, par exemple toutes les 15 minutes.
5. Procédé suivant revendication 1, caractérisé en ce que le deuxième sorbant est chargé à proximité immédiate d'un ventilateur de tirage par aspiration, de préférence dans ce ventilateur.
6. Procédé suivant revendication 1, caractérisé en ce que le sorbant séparé par le filtre en tissu et partiellement chargé est injecté dans le premier étage de purification dans la zone de la chambre de combustion.
7. Procédé suivant revendication 1, caractérisé en ce que la quantité introduite du deuxième sorbant est réglée suivant le contenu en gaz polluant du gaz de fumée à la sortie de l'installation de combustion et particulièrement du deuxième étage de purification.
8. Installation de combustion avec purification de gaz de fumée aval équipée de points d'alimentation de sorbants dans la zone de la chambre de combustion (1) et après elle pour l'exécution du procédé suivant au moins une des revendications 1 à 7, caractérisée en ce que dans la zone du gaz de fumée partiellement refroidi entre l'électrofiltre, le cyclone ou cyclone multiple (2) et un filtre en tissu (6) un deuxième point d'alimentation (12') est prévu pour un deuxième sorbant dont la composition chimique diffère de celle du premier sorbant.
9. Installation de combustion suivant revendication 8, caractérisée en ce que l'alimentation (12') du deuxième sorbant avant le filtre en tissu (6) est prévue à proximité immédiate d'un ventilateur de tirage par aspiration (3) (Fig. 2).
10. Installation de combustion suivant revendication 8, caractérisée en ce qu'une conduite de recirculation (15) menant au premier étage a été prévue pour le sorbant partiellement usé qui est séparé par le filtre en tissu (6).
11. Installation de combustion suivant revendication 8, caractérisée en ce que l'alimentation (12') du deuxième sorbant du côté du gaz brut directement avant le filtre en tissu (6) est construit sous forme de tuyère d'injection (19).
EP19850900002 1983-11-25 1984-11-23 Procede de separation de gaz polluants acides et installation de combustion Expired EP0162085B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
AT4136/83 1983-11-25
AT413683A AT380645B (de) 1983-11-25 1983-11-25 Verfahren zur abscheidung von sauren schadgasen und verbrennungsanlage zur durchfuehrung des verfahrens

Publications (2)

Publication Number Publication Date
EP0162085A1 EP0162085A1 (fr) 1985-11-27
EP0162085B1 true EP0162085B1 (fr) 1988-07-27

Family

ID=3560140

Family Applications (1)

Application Number Title Priority Date Filing Date
EP19850900002 Expired EP0162085B1 (fr) 1983-11-25 1984-11-23 Procede de separation de gaz polluants acides et installation de combustion

Country Status (7)

Country Link
EP (1) EP0162085B1 (fr)
AT (1) AT380645B (fr)
DD (1) DD223073A5 (fr)
DE (1) DE3473030D1 (fr)
DK (1) DK340285D0 (fr)
HU (1) HU194981B (fr)
WO (1) WO1985002453A1 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3911767A1 (de) * 1989-04-11 1990-10-25 Teset Thermo En System Entsorg Verbrennungsanlage fuer fossile brennstoffe, insbesondere fuer muell

Families Citing this family (24)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS60216832A (ja) * 1984-04-10 1985-10-30 Hitachi Zosen Corp 乾式石灰法による排ガスの浄化方法
EP0190416A3 (fr) * 1984-11-30 1988-07-27 Waagner-Biro Aktiengesellschaft Procédé de séparation de polluants de gaz brulés
FR2579111A1 (fr) * 1985-03-25 1986-09-26 Mediterranee Const Navales Ind Procede d'epuration des fumees des usines d'incineration d'ordures menageres
DK548786A (da) * 1985-11-28 1987-05-29 Aalborg Vaerft As Fremgangsmaade til rensning, navnlig afsvovling, af roeggas
SE456642B (sv) * 1986-06-03 1988-10-24 Euroc Research Ab Saett foer direkt avsvavling av roekgaser i en eldstad
DE3635027A1 (de) * 1986-10-15 1988-04-28 Steinmueller Gmbh L & C Direktentschwefelungsverfahren mit flugstaubrueckfuehrung
FI76931B (fi) * 1986-12-12 1988-09-30 Imatran Voima Oy Foerfarande foer rening av roekgaser.
JP2602085B2 (ja) * 1987-05-18 1997-04-23 エフテーウー ゲーエムベーハー フォルシュング ウント テヒニッシェ エントヴィックルング イム ウムヴェルトシュッツ ガス及び廃ガス浄化用の反応性水酸化カルシウム基浄化剤並びにガス及び廃ガスの浄化方法
SE461380B (sv) * 1987-09-30 1990-02-12 Asea Stal Ab Saett och anordning att foerbaettra utnyttjningsgraden av en ca-haltig svavelabsorbent i en kraftanlaeggning
DK153888A (da) * 1988-03-21 1989-09-22 Fls Miljoe A S Fremgangsmaade til forbraending af affald
EP0377010A1 (fr) * 1988-05-16 1990-07-11 Ftu Gmbh Agent et procede pour purifier des gaz et des gaz d'echappement, et procede pour produire ledit agent
AT393232B (de) * 1989-11-24 1991-09-10 Voest Alpine Ind Anlagen Verfahren zum entfernen von schadstoffen aus heissen produktgasen
EP0454885A1 (fr) * 1990-05-02 1991-11-06 Ftu Gmbh Procédé pour la purification de gaz et de gaz d'échappement de polluant
WO1992003212A1 (fr) * 1990-08-17 1992-03-05 Fritz Schoppe Procede et dispositif d'amelioration de l'utilisation de la chaleur degagee par des gaz de combustion contenant des poussieres ou des cendres
AT394733B (de) * 1990-10-16 1992-06-10 Voest Alpine Ind Anlagen Verfahren und anlage zur herstellung von fluessigem stahl aus schrott und anlage zur durchfuehrung des verfahrens
US5500195A (en) * 1992-11-13 1996-03-19 Foster Wheeler Energy Corporation Method for reducing gaseous emission of halogen compounds in a fluidized bed reactor
AT404182B (de) * 1993-06-03 1998-09-25 Ica Innoconsult Ag Korrosionsschutzverfahren für verbrennungsanlagen
DE4344112C2 (de) * 1993-12-23 1998-10-22 Metallgesellschaft Ag Verfahren zur Steuerung der Sorptionsleistung eines Filtrationsabscheiders
EP0716264B1 (fr) * 1994-12-06 2000-08-30 L. & C. Steinmüller GmbH Procédé et installation pour la combustion des boues
DE19531379C1 (de) * 1995-08-26 1997-05-28 Petersen Hugo Verfahrenstech Verfahren zur Verbrennung von Klärschlamm und Anlage zur Durchführung des Verfahrens
FR2751560A1 (fr) * 1996-07-26 1998-01-30 Solvay Procede pour epurer une fumee contenant du chlorure d'hydrogene, un oxyde d'azote ou du dioxyde de soufre
FR2814533B1 (fr) 2000-09-27 2002-10-31 Alstom Power Nv Procede pour reduire simultanement les emissions de co2 de so2 dans une installation de combustion
DE102014118767A1 (de) * 2014-09-29 2016-03-31 ReNabi GmbH & Co. oHG Verfahren zur Behandlung von Abgasen
CN104492244A (zh) * 2014-12-17 2015-04-08 国网上海市电力公司 一种废气处理设备

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR1424831A (fr) * 1965-02-17 1966-01-14 Escher Wyss Sa Soc Procédé et dispositif pour empêcher l'émission de gaz sulfureux et sulfurique avec les gaz d'échappement d'un foyer
FR2285169A1 (fr) * 1974-09-19 1976-04-16 Mitsubishi Heavy Ind Ltd Procede de controle de la corrosion des appareils de traitement des gaz venant des fours verriers
DE3106580A1 (de) * 1981-02-21 1982-09-02 L. & C. Steinmüller GmbH, 5270 Gummersbach Verfahren zur minimierung der emission von verunreinigungen aus verbrennungsanlagen
DE3106526A1 (de) * 1981-02-21 1982-09-16 L. & C. Steinmüller GmbH, 5270 Gummersbach Verfahren zur minimierung der emission von verunreinigungen aus verbrennungsanlagen
DE3308927A1 (de) * 1983-03-12 1984-09-13 L. & C. Steinmüller GmbH, 5270 Gummersbach Verfahren zur bindung von in rauchgasen enthaltenen gasfoermigen schadstoffen

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3911767A1 (de) * 1989-04-11 1990-10-25 Teset Thermo En System Entsorg Verbrennungsanlage fuer fossile brennstoffe, insbesondere fuer muell

Also Published As

Publication number Publication date
HU194981B (en) 1988-03-28
ATA413683A (de) 1985-11-15
EP0162085A1 (fr) 1985-11-27
WO1985002453A1 (fr) 1985-06-06
HUT37249A (en) 1985-11-28
AT380645B (de) 1986-06-25
DD223073A5 (de) 1985-06-05
DK340285A (da) 1985-07-25
DK340285D0 (da) 1985-07-25
DE3473030D1 (en) 1988-09-01

Similar Documents

Publication Publication Date Title
EP0162085B1 (fr) Procede de separation de gaz polluants acides et installation de combustion
DE3428502C2 (fr)
EP0828549B1 (fr) Procede de desulfuration a sec d'un gaz de combustion
DE2931169A1 (de) Verfahren zur beseitigung von sauren komponenten aus abgasen
EP0694328A2 (fr) Procédé pour la purification de gaz d'échappement
DE69503378T2 (de) Entfernung saurer gase und partikeln bei hoher temperatur im müllverbrennungsverfahren
DE4233303C1 (de) Verfahren zur Abtrennung von Dioxinen und Furanen aus Abgasen von Verbrennungsanlagen
DD262593A5 (de) Verfahren zum reinigen von schadgasverbindungen enthaltendem abgas
EP0743875B1 (fr) Procede et systeme d'epuration non-polluante de gaz de fumee
DE3527615A1 (de) Verfahren und anlage zur entsorgung von chlorhaltigen abfaellen, insbesondere von haus- und kommunalmuell
DE3942092A1 (de) Verfahren zur reduzierung des no(pfeil abwaerts)x(pfeil abwaerts)-gehaltes in abgasen
DE69931924T2 (de) Verfahren zur reinigung von abgas
DE2934109A1 (de) Verfahren zur trockenen behandlung von abgasstroemen in abgasreinigungssystemen
EP0289810B1 (fr) Procédé de retention de mercure des gaz brûlés d'une installation de combustion
DE3235020A1 (de) Chemisorptionsverfahren zur absoprtion von vorzugsweise schwefeldioxid hinter kraftwerken und muellverbrennungsanlagen und dergleichen
DE3015977A1 (de) Verfahren und vorrichtung zur trockenen chemisorption hinter feuerungskessel- oder wirbelbettanlagen
DE3608920A1 (de) Verfahren zur herstellung von koernigen mineralstoffen aus kohleabbraenden
DE4409057C2 (de) Verfahren zum Betrieb einer druckaufgeladenen zirkulierenden mit Braunkohle betriebenen Wirbelschichtfeuerung für ein Kombikraftwerk
DD239127A5 (de) Verfahren zum entschwefeln von rauchgasen
EP0672020B1 (fr) Procede et installation de sechage suivi de dissociation
DE3702463A1 (de) Kombiniertes trocken und nass arbeitendes rauchgasreinigungssystem zur abscheidung von hf, hcl, so(pfeil abwaerts)3(pfeil abwaerts), so(pfeil abwaerts)2(pfeil abwaerts), no(pfeil abwaerts)x(pfeil abwaerts) und staub
WO2001038815A2 (fr) Procede de nettoyage de la surface d'un echangeur thermique et agent de sablage utilise
DE3741842C2 (de) Verfahren zur Verminderung der bei der Verbrennung entstehenden gasförmigen Schadstoffe SO¶x¶, HF und HCl
DE3329972C2 (fr)
AT383504B (de) Verfahren und einrichtung zur abscheidung von sauren schadgasen

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

17P Request for examination filed

Effective date: 19850725

AK Designated contracting states

Designated state(s): BE CH DE FR GB LI LU NL SE

17Q First examination report despatched

Effective date: 19860429

GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

AK Designated contracting states

Kind code of ref document: B1

Designated state(s): BE CH DE FR GB LI LU NL SE

REF Corresponds to:

Ref document number: 3473030

Country of ref document: DE

Date of ref document: 19880901

GBT Gb: translation of ep patent filed (gb section 77(6)(a)/1977)
ET Fr: translation filed
PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: LU

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 19881130

PLBE No opposition filed within time limit

Free format text: ORIGINAL CODE: 0009261

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT

26N No opposition filed
PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: SE

Payment date: 19891017

Year of fee payment: 6

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: BE

Payment date: 19891115

Year of fee payment: 6

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: LI

Effective date: 19891130

Ref country code: CH

Effective date: 19891130

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: NL

Payment date: 19891130

Year of fee payment: 6

Ref country code: GB

Payment date: 19891130

Year of fee payment: 6

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: FR

Effective date: 19900731

REG Reference to a national code

Ref country code: CH

Ref legal event code: PL

REG Reference to a national code

Ref country code: FR

Ref legal event code: ST

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: GB

Effective date: 19901123

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: SE

Effective date: 19901124

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: BE

Effective date: 19901130

BERE Be: lapsed

Owner name: WAAGNER-BIRO A.G.

Effective date: 19901130

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: NL

Effective date: 19910601

NLV4 Nl: lapsed or anulled due to non-payment of the annual fee
GBPC Gb: european patent ceased through non-payment of renewal fee
EUG Se: european patent has lapsed

Ref document number: 85900002.8

Effective date: 19910705

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: DE

Payment date: 19951020

Year of fee payment: 12

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: DE

Effective date: 19970801